Process for treating oils



Oct. 29, 1935. J Q BLACK PROCESS FR TREATING OILS Original Filed Oct. 13

- INVENTOR.

CI C/ac/i BY v d RNEYS.

NN NN NMS n, M,

KMQUUQ Patented Oct. 29, 1935 PATENT OFFICE rnocnss Fon 'raEA'rrNG oms John C. Black, .Los Angeles, Calif., assignor to Gasoline Products Company, Inc.. Wilmington,

Del., a corporation ot Delaware Application October 13, 1926, Serial No. 141,419

Renewed November 2, 1932 13 Clalml.

This application is a continuation' in part of application, Serial Number 116,217, iiled June In my Patent 1,456,419, there is described a process for thel production o! lower boiling point .Y passes.

hydrocarbons from those of higher boiling point which comprises preheating the oil in a-heating coil tothe point of active decomposition and then subjecting the thus heated oil to a further heat treatment where it is maintained at the temperature attained in the preheating coil, or at a higher temperature, and the endothermic heat of the cracking reaction supplied.

In passing through the second heatingl or cracking coil the hydrocarbons are subjected to the cracking temperature and maintained for a suiicient length of time to obtain the desired cracking eects. The stream of oil is kept'under suiiicient pressure to prevent substantial vaporil zation. The hydrocarbons passing from the cracking or reaction coils are then passed-either to a carbon settling chamber or reaction chamber for the further decomposition and carbon deposition, or the cracked oil passing `irom the heating coil may be sent directly through a pressure reducing and discharge valve and from thence immediately into a iractionating apparatus.

The invention which is the subject matter of this application utilizes the general method above outlined, and has for one oi its objects the regulation of the thermal and cracking eects which take place in the nal passes oi' the cracking coil. In the previously mentioned application, of which this application is a continuation .in part, this regulation `may be effected by splitting the heated stream and passing one of the split streams, called the bypass stream, into vthe nal passes of the cracking coil.

Other methods are described whereby oil o1 any desired temperature, from cold unheated oil to relatively highly heated oil, may be introduced into the final passes. I have found that in operating the process as described in my Patent 1,456,419, that the nal passes of the reaction coil tend to foul with carbon and after a period the apparatus has to be shut down and cleaned. I have found by the injection of this 0 oil into the nal passes, I obtain a greater yield of decomposed hydrocarbons. I have found also that the fouling oi' the tubes is very materially lessened by this injection of the oil into the final I have also found that the injected hydrocarbons are themselves partially 'decomposed by the heat contained in the hydrocarbons `becomes more and more severe. This is aggraof the main stream into which they are injected,` and also by the heating eiect derived from the furnaces while passing through lthe nal passes of the reaction coil. By this injection oi oil the heat absorptive characteristics of the oil stream e is modiiled and heat may be transferred to the oil stream without excessive carbonization resulting. l

While I do not limit myself to the theory here advanced, I believe that this theory is a very 1o probable explanation oi' the phenomena observed. It is apparent -that in operating the streams according to my former method, without the injection of oil to the iinal passes, that the' ol, reaching the iinal passes, will have been high- 15 ly cracked with a large formation of lighter oils which do not crack easily. The oil stream also contains heavy bodies, probably formed as a result of the cracking reaction. The practical oil man says that the oil becomes dirtyy The oil zo stream and the re are manipulated so as to maintain the oil at the chosen cracking temperature. Any transfer of heat that results under the above circumstance goes to carbonize the heavy bodies, depositing a dense carbon on the 2t;`

walls of the tubes. The heat conductivity is thus reduced. The tubes become overheated and-,v

the result is that as more oil advances the carbonization at the lm between the oil and tubes 30 vated by the fact that in systems involving counter-current passage of oil and combustion gases in the furnace, the oil in the nal passes of the coll cornes in contact with the hottest gases.A

Another result is that this high temperature 35' cracking which results at the surface of the highly heated tubes causes a formation oi a large amount of gas which builds up a high vapor pressure. This pressure, if carried to excess, may vexl ceed the operating pressure employed ancl'cause 40 a serious interference in the operation oi.' thel process. 'Ihe introduction of cold or relatively cold uncracked oil into the final passesavoids the diillculties mentioned above. The injected oil absorbs heat, in having its sensible heat aug- 4,5

` mented, from the cracked oil entering the nal passes, thereby lowering the temperature of the cracked oil and also checking its crackin-g. They partially cooled stream then absorbs heat from the combustion gases and the tube Wall surfaces() to have its temperature raised to substantially the desired cracking reaction. 'Ihere is, therefore, under these circumstances a large transfer of heat from the combustiongases to the oil passing through the final passes of the coile The u uncracked oil in the stream also absorbs heat due to the endotherrnicl character of the cracking reaction. 'I'he tubes are kept from overheating and the excessive carbonization as above described is materially reduced.

Furthermore, by the injection of this relatively cold oil, any carbonaceous material deposited in the reaction is of softer composition and is more readily removed in the blowing down operation and the heaters can be put back on stream-with a smaller loss of time. The injected oil should be so controlled that the temperature of the admixed streams may be such that the decomposition of the injected oil is partially accomplished and to obtain a temperature of the mixture such that the decomposition in the main stream is checked and the carbon of decomposition is minimized.

In the operation which forms the subject matter of this application, I prefer to use an unheated ollas the injection oilinsteadof using. a partially heated oil, bypassed from the partially heated main stream. By so doing I can limit the amount of injected oil I need to be much less than if I were touse the above bypassed partially heated stream. I have also found that the cracking effect upon the injected oil is greater when I use cold oil rather than partially heated oil. While I do not wish to be limited by my theory, I becontinuous system wherein crude oil may be converted to gasoline. This process consists Aessentially of separating a cracldng stock from the crude, and decomposing this cracking stock by the process described above, and to be more-completely described later. This cracking stock is obtained by distilling the oil by a process involving the heating of the oil in tubes and the evaporation of oil in an evaporator connected to a fractionating device. While this oil may be heated `in any desired manner, I prefer to heat the oil by the waste gases coming from the main cracking coils in which the cracking stock is decomposed. The process also involves the control of the fractionation of both the crude oil and cracking material Vby heat exchange with the cold crude oil. l

Another object of this invention is to devise an apparatus for carryingout the process discussed above.

The process and apparatus may be better understood by reference to the accompanying drawing showing systematically an apparatus for carrying out this process.

In the drawing:

I is a crude oil storage tank. 2 is a transfer line in which there is a valve 2. This transfer line is connected to a pump 3. s4 is a line leading from pump 3 to analyzer I0. 4 is a valve therein.

denser '2I. 6 is a by-paas line controlled b! valve II is a transfer line from analyzer Il! leading to coils I2 and I3 situated in the furnaces I4 and I5, respectively. I6Ais a transfer line con necting coil I2 to evaporator I1.

6' for by-passing oil around analyzer I 0 direct to coils I2 and I3. Line6 which is controlled by valve 6' connects pump 3 with analyzer 1 in bubble tower 46 whereby oil may be passed through analyzer 1, and the amount of oil passing to ana- 5 lyzers 1 and I0 controlled. 8 and 8 are transfer linesconnecting analyzer 1 to-coil I2, Pump I8' takessuction on the liquid in evaporator I1. 26v is a line connecting pump I8 to heat exchangerv A. 21 is a line connecting exchanger A to tank 10 28. 28 is a line connecting the liquid trap I8 in bubble tank I1 to cooler 30. 3| is a tank for storing the liquid from cooler 30. 32 is a line connecting the pump 33 to tank,3l. 32' is a valve in line 32. heat exchanger A. Line 35 connects exchanger A with exchanger B. Line 34 is' controlled by a valve 34. 36 is a line connecting heat exchanger B with heat exchanger C. 36' is a valve in said line. 31 is a line connecting heat exchangerC go with line 38, which line leads to coil 38, situated in furnace I5. '48 is a coil situated in furnace I4 and connected to coil 38. 4| is a cross over line connecting coil 48 to the carbon catcher and reaction chamber ,42. 4|' is a valve in said line. 25 43 is a line connecting carbon catcher and reaction chamber 42 with exhanger C and evapora- 4tor 45.

I have also shown a cross over connection 68 controlled by valve 68 whereby the carbon catchaci er and reaction chamber may be by-passed. As a matter of practical construction I prefer to build the apparatus either with or without the carbon catcher, thus avoiding valves 4I', 431- and 68', since it is desirable to out down the number sa: of valves exposed to hot oil. I have merely shown this connection to indicate that the processA 'may be operated with lor without carbon catcher. However, this by-pass may be put on as special precautions are taken as to the character of the 40:A

valves employed. -f

43"' is a pressure reduction valve in line 43, 46 is a fractionating tower connected to evaporator 45. v10 is a liquid trap in evaporator 45.- 41 is a vapor line connecting the fractionating tower and yf5-i condenser 48. 48 is a look box connected to condenser 48 through which condensate flows from f condenser 48 to tank 50.- 1I is a gas main for collecting the uncondensed gases rising from look box- 48. 55 is ,a line connecting the liquid trap 50" 18 with cooler 56 from.which cooled'oil passes to tank 51. 58 is a line controlled by valve 58' connecting-tank 51 and pump 33. 5I is a line conf trolled by valve 51' connecting line 34 and the final passes of the reaction coil 40. 52" is a valve 5'5- controlling the passage of oil from 5I to the final passes of the reaction coil. 52" is a by-pass valve controlling the passage of'oil to the final tube ofthe final pass of the cracking coil. 53'is a bypass line connecting line 5I to line 4I. Line 5360 is controlled by`valve 53. As a matter of practical construction I prefer to eliminate valves 82 and 53' and to build the plant 'with one of the three alternative methods of oil injection. 54 I is a line controlled by valve 54 connecting line 36 65 to line 38 for by-passing exchanger C. 58 is a line connected to theibovttomJ of the evaporator 45 and also connected to pump 60. 6I is-.a`line connected to pump 68 and passingthrough exchanger B and leading to tank 62. 63 is a water 70' tank. 65 is a line connecting this water tank to line 54. 64 is a pump in said line and 65',v is a valve in said line. 66 is a pressure recorder in line 43 and arranged immediately` before valve 43". 61 is a pressure recorder in line 34 arranged 15 34 is a line leading from pump 33 to 15 between pump 33 and valve 34. 68 is a pyrometer located in line I6. 12 is a pyrometer located at the exit point of coil 39. 13 is a pyrometer located at the4 point of admission of oil passing through valve 52. 14is a pyrometer located in the entrance point of the carbon catcher and reaction chamber 42. 69" is a, pyrometer located at the exit point of the cracking coil 40. 15 4is a line connecting tank 25 with the upper trays of tower I9. Valves 15 and 15 and pump 16 controls the passage of condensate in this line. 11 is a line connecting tank with the upper trays in tower 45. 'I1' and 11" are valves in said line. 18 is a pump in line 11. l

The operation of the process will be understood in connection with the above description. Crude oil is picked up by pump 3. It may be then passed through line 4, analyzer I0, coils I2. and I3, or some or all of it may be by-passed via line 5 direct to coils l2 and I3, depending upon the necessary control required in bubble tower I9. The regulation of the amount of oil passing through the analyzer I0 controls the character of the fractionation in fractionator I9. Oil may also be passed via line 5to analyzer 1. The amount of oil thus passed controls the character of the fractionation in fractionator 46. Oil from 1 is then passed via 8 and 9 to coils I2f'and I3. The oil is heated in coils I2 and I3 by the waste combustion gases rising in 30 furnaces I4 and I5. The temperature of the oil leading from I2 and I3 is controlled in order to obtain the desired temperature at the point indicated by pyrometer 68. This temperature is preferably above 500 F. Since the waste heat gases are usually above 1,000 F., ample heat is obtainable to obtain the desired temperature at point G9.

The heated oil then passes to evaporator I 1. ,Uni y vaporized material is drawn off through line I8.' and pump I9 and passed via line 26, through exchanger A and line 21, to the crude oil residue tank 28. Vapor rising through tower I9 is fractionated and the reflux condensate formed is collected in I8, drawn off through line'29, through cooler 33 to the gas oil tank 3 I.

This middle fractionate is a gas oil which is preferably of a character required for the-cracking process. The fractionation and distillation in Iland I9 is so controlled as to give the desired condensate in I 8 to be drawn oi as a lcracking stock. This is obtained by controlling the temperature of the oil passing to I1 and the quantity of oil passing through analyzer vI 9 and also by introduction of rei-lux oil into I9, as for instance condensate from 25, via line 'I5 and pump 16.

I prefer to use a gas oil as a cracking stock and I have, therefore, marked tank 3| as a gas oil tank. The condensate may, however, be of any desired character, depending upon the needs of the cracking system. Vapors rising in I9 are fractionated as previously described, and uncondensed vapor passes through 20 to becondensed in 2l,

-and condensate collected in 25. This condensate heat exchanger A, where it abstracts heat from residuum from I1. The oil is then passed through B via 35 where it abstracts heat from residuum from 45, and is then passed through C where it abstracts heat from the cracked oil. A

part of the oil may be by-passed around heat exchanger C in arder to regulate the heattransfer which occurs in heat exchanger C. The oil is then passed into coil 39 where it is heated up to the reaction temperature by the combustion gases in the furnace, which reaction temperature is marked Vby pyrometer 12, and then passed through V5 coil 40 where the endothermic heat of the cracking reaction is supplied. 'Ihe heating in coil 4a is controlled to maintain at least the temperature which was indicated at 12. Preferably this temperature is maintained throughout coil 4U with the 1o modification described later. Coils 39 and 40 may be part of one coil in a single furnace, but I prefer to have them in separate furnaces since this enables a better control of the heating of the coils and the oil passing therethrough.

While I have shown the 'heating arrangement as based on the countercurrent principle, I do not limit myself to this arrangement, this invention being applicable to any arrangement of coils in a lli' furnace, wherein oil is heated by hot combustion 20'- gases. v A

The oil issuing from the coil ,43 is cracked tothe desired degree. It may then be passed to the carbon catcher and reaction chamber 42 or passed directly to heat exchanger C. The oil, in passing 35 through exchanger C, is'cooled down to the de' sired temperature in order to obtain the charac-l ter of evaporation desired in the vaporizer 45. There is a reduction of pressure at the point of the valve 43". The unvaporlzed material remains 30'.

in the vaporizer' 45, and the vaporized material passes through t5 to .be fractionated. A condensate is formed and collected in 10 and uncondensed material passes through pipe 41 to be condensed in 38 and collected vla look box 49 in tank 35" sage through 1 and maybe further controlled by 45:

introduction of reflux oil into fit, as for instance, condensate from 5@ via pipe 11 by pump 18. The stream passing through line 34 may be split to withdraw a portion of the oil via line 5i to be injected into the nal passes of the reaction coil. 50 While I have shown this oil as injected in thelast pass, it is understood that this is merely schematic andthe oilmay be injected in any one of the numerous passes depending how long it is desired that the mixed ons be heated by the combustion 55."

gases, and also when it is desired to modify the heat abs'orptlve characteristics of the stream by reducing its temperature and checking the cracking of the heated oil. The amount of oil which is by-passed and injected into the final passes is 601' controlled so that the temperature recorded by pyrometer 13 shall be at the desired point.

Oil may also be injected into the transfer line connected with the carbon catcher when that is employed, or may be also injected in. the transfer 65 line 4I, even when the carbon catcher is not ernployed, to control the temperature of the oil passing through line 43. 'I'his by-pass ol' oil via 53 may be employed even when the by-pass via 52 is not employed. Instead of injecting oil at the outlet of the cracking coil, ltmay be injected into the nal .tube or tubes of the nal pass of the cracking coil.' I have also shown a connection for blowing out the system in order to clear it of any collected` 75 carbon. This pump 64 picks up water from tank 63, passesit through line 65, via 65', into line 34,

valves 36 and 54 being closed. The water is then passed through coils 39 and 40 and reaction chamber 42, valves 69', I3' being closed and is blown down to a blow-down line as indicated. When the reaction chamber is not employed the blow-down is made via pipe 69 into the evaporator and the water is by-passed to the sewerto avoid contamination of the residuum in 62. 'Ihis blowdown process is the vsame as shown in my previouslynientioned patent.

" and 10% of residue and the rest is gas and loss.

The crude oil is passed through the coils I2 and I3 at about a pressure of 50 pounds or just sumcient to force the crude oil through the tubing and .to the evaporator. The waste heat gases passing uplthroughrthe 'furnaces I3 and I4 reach coils I2 and I3 at atemperature of about 1,000".

'The oil is heated in the coils, and is passed to the evaporator I1 at a temperature of about 500 F.

I operate this system in such manner that the oil collected in trap I8 and drawn oil' through line v2li is a gas oil or other desired oil suitable for cracking in the system. This oil, together with the cycle oil, is passed with such a pressure that the recorder 66 will show approximately 1000 pounds, or suicient to overcome the vapor pressure -in the coils so as to ensure a liquid phase condition in the coils. 'I'he pump pressure is usually higher than'A that depending on the fric- .tional resistance of thevsystem, i. e. of the tubes and heat exchanger. Usually this resistance varies from 200 pounds to 500 pounds, depending upon how foul /the system is. 'I'he oil passing through coils 39 is heated up to the reaction temperature which is chosen for that oil to obtain optimum lresults. The thus heated oil is passed to coil 40 where it is maintained at the reaction temperature for the desired length of time, the

time factor depending upon the speed of the oil and the length and character of the tube. Both these factors are `controlled to give the desired Kcracking effects, that is, to obtain a cracked oil containing the desired amount of low boiling hydrocarbons, and which will give a residue on distillation vof the desired viscosity and boiling range and carbon content. y The temperatures maintained in the passage through the cracking coil 40 `vary between 800 and 900 F., depending upon the oil, and is preferably approximately equal to the temperature of. the oilat point 12, but may be higher than that temperature. It is important, however, to supply at least the endothermic heat of the cracking reaction during the passage of the oil through coil I0; 1 r

Cold oil is injected at 52 .to bring this temperature down to about 800, read at point 13, and the mixed oil is heated from this point to the required maximum temperature as it flows through the final passes of the coil. This injection of oil and heating is controlled to give the desired cracking temperature which is read at point 69". The injection of the oil at point 52' checks the cracklng ofthe main stream of oil and also causes a I claim to be:

cracking of the injected oil. It also controls the thermal eiects as described previously.

Oil may also be injected into line 4I just the other side of the cracking coil in order to control the temperature of the oil passing to the carbonv d catcher or to the evaporator. This will also crack the injected oil as a result of the heat abstracted from the main stream. Oil may also be injected via 52". This controls the cracking in the nal tube or tubes and also acts to crack the injected l0 oil. As previously thiscrackng is also aiected by the -shock phenomenon.

-The oil passing through heat exchanger C is cooleddown by the oil passing through heat exchamber via lines 36 and 31. By-pass 54 is controlled so that the amount of oil passing through C via lines 36 and 31 shall be such that the oil passing through the evaporator shall not be cooled down below its proper vaporization point which may be 600 F. This temperature is required to 20 insure as complete a vaporization, as possible and to limit the amount of residue in the evaporator.

While I have shown the oil injected into the iinal passes as being of the same character as that l passed to the coils 39 and 40, this is only one way 25 'I'he above description is not to be taken as limiting of my invention, but merely illustrative of the best method of using my invention, which 1. A continuous process lof cracking ,and dis- 40 tilling hydrocarbon oil which comprises passing theoil under pressure to and through a coil, heating said coil by gases of combustion to crack the oil; passing other oil through another coil; heating said lastmentioned coil by waste gases of combustion resulting from the heating of the nrst mentioned coil; fractionating said second mentioned oil into several fractions and injecting a portion lof the heavier distillate fraction thus formed into the first mentioned coil in the desired quantity into the final passes thereof, to preve'nt excessive decomposition of the hot oil therein, and to crack the injected oil to the desired degree. 2. A continuous process for cracking and distilling oil which comprises heating oil under pressure, to a cracking temperature in' a coil in the relatively hot' section of a furnace; vaporizing the oil fractionating and condensing the vapors and withdrawing the condensate; heating and vaporizing a partof another oil in another coil in a relatively cooler section of said furnace; fractionating said other oil and separately withdrawing from the fractionating zone a residuum, a condensate and lower boiling hydrocarbon vapors; injecting a portion of said last namedcondensate into the ilnal passes of the first mentioned coil; said ilnal passes containing the hottest oil,

- -to prevent over-cracking of the hot oil in said iinal passes, and cracking the cool injected o byI raising its temperature suddenly -to a cracking degree.

3. A continuous processv for cracking and distilling oil which comprises passing oil under pressure, suillcient toprevent any substantial v'aporization, to and through a con; heating the ou to a 7 portion thereof to the coil for re-cracking; passl ing crude oil containing gasoline hydrocarbon fractions through a second coil situated in the path of waste combustion gases from the first mentioned cracking coil; vaporizing a portion of said oil and fractionating the vapors in a second fractionating zone; condensing and withdrawing the lighter fraction; condensingand cooling the heavier fraction and returning a portion of said heavier fraction to the final passes of the rst mentioned coil, to prevent overcracking of the hot oil therein and to heat said heavier fraction to a cracking temperature.

4. A continuous process for cracking and distilling oil which comprises passing oil under pressure, suiiicient to prevent any substantial vaporization, to and through a coil; heating the oil to a predetermined cracking temperature; vaporizing a portion of said oil and fractionating the vapors; condensing and withdrawing the lighter lfraction; condensing the heavier fraction and returning a .portion thereof to the coil for recracking; passing crude oil containing gasoline I hydrocarbon fractions through a second coil situated in the path of waste combustion gases from the first mentioned cracking coil; vaporizing a portion of said oil and fractionating the vapors in a second fractionating zone; condensing and withdrawing the lighter fractions; condensing and. cooling the heavier fraction and returning a portion of said heavier fraction to the outlet of the final passes of the first mentioned coil to prevent overcracking of the hot oil therein.

5. A continuous process of cracking and distilling hydrocarbon oil which comprises passing the oil under Vpressure to and through a coil, heating said coil in aI furnace by gases of coin-- bustion to crack the oil, discharging from the coil the stream of cracked products into a separating zone wherein vapors and liquid residues are separated, passing other oil through another coil, heating said last mentioned coil by gases of combustion in the said furnace,` separating the said second mentioned oil into several fractions differing with respect to their boiling point ranges and injecting a portion of a higher boiling fraction thus formed while below substantial cracking temperature into the outlet of the first mentioned coil in the desired quantity, to prevent excessive decomposition of the hot oil therein, and-to crack the injected oil to the desired degree.

6. A continuous process for cracking and distilling oil which comprises passing oil under pressure, sufficient to prevent any `substantial vaporization, to and through a coil in a heating zone, heating the oil to a predetermined cracking temperature, passing the oil from the coil into a separating zone wherein vapors and liquid separate, fractionating the separated vapors, condensing and withdrawing the lighter fraction, condensing the heavier fraction and returning a portion thereof to the coil for re-cracking, passingpcrude oil containing fractions suitable as cracking stock through a second coil heated by the said heating zone for the first mentioned cracking coil, vaporizing a portion of said oil and fractionating the vapors in a second fractionating zone, condensing and withdrawing the lighter fraction, condensing and cooling the heavier fraction and returning a portion of said heavier fraction to the final passes of the first mentioned coil to prevent overcracking of the hot oil therein and to heat said heavier fraction to a cracking temperature.

7. A continuous process for cracking and distilling oil which comprises passing oil under pres- 5 coil into a separating'zone wherein vapors and 10 liquids separate, fractionating the separated vapors, condensing and withdrawing the lighter fraction, condensing the heavier fraction andreturning a portion thereof to the coil for re'- cracking, passing fresh oil containing hydrocar- 15 bon fractions suitable as a cracking stock through a second coil situated in the path of combustion gases employed in heating the said first mentioned cracking coil, vaporizing a portion of said oil and fractionating the vapors in a second fractionating zone, condensing and withdrawing a lighter fraction, condensing and cooling a heavier fraction, and returning a portion'of said heavier fraction to the outlet of the final passes of the rst mentioned coil to prevent overcracking of 25 the hot oil therein.

8. A continuous process for cracking and distilling oil which comprises passing oil under pressure suflicient to prevent any substantial vaporization, toand through a coil, heatingI the oil to a predetermined cracking temperature, passing the oil from the coil into a separating zone wherein vapors and liquid residues are separated fractionating the 'separated vapors, condensing oil containing gasoline hydrocarbon fractions through a second coil situated in the path of gases employed in heating the .first mentioned cracking coil, vaporizing a portion of said oil and fractionating the vapors in a second fractionating zone, condensing l and withdrawing the lighter fractions, condensing and cooling the heavier fraction 'and returning a portion of said heavier 45 fraction to the nal passes of the first mentioned coil to prevent over-cracking of the hot oil therein and to heat said heavier fraction to a cracking temperature.

9. A process of distilling and-converting hydro- 5@ carbon oils which comprises passing hydrocarbon oil through a pipe coil heated by hot combustion gases where it is subjected .to cracking under a relativelyhigh pressure, discharging the cracked highly heated oil from said coil into a rela- @5 tively low pressure separating zone, passing evolved vapors from said separating zone to a fractlonating operation wherein heavier constituents of said vapors are condensed as reux condensate and thereby separated from desired lighter constituents of saidvvapors, withdrawing said reflux condensate from said fractionating operation and forcing it through said coll whereby it is subjected to cracking and subsequently passed to said vaporizing zone, simultaneously passing another oil @5 through a separate coil exposed' to combustion gases employed in heating said rst-named coil and heating it during its ow therethrough to a distilling temperature, discharging the heated oil from the latter coil into a separate combined vas porizing and fractionating zone wherein higher boiling constituents of said oil are separated and collected in liquid'form and desired lower boiling constituents are separated in vapor form, sepy arately withdrawing the said separated desired im v i sure to a crackingl temperature in a coilin the` v cracking coil and saidfirst-named separating zone to check cracking of the said oil stream.

10. 'I'he process of distilling and converting hydrocarbon oils which comprises passing hydrocarbon oil through a pipe coil heated by hot combustion gases wherein it is subjected to cracking under a relatively high presure, discharging the cracked highlyheated oil from said coil into a relatively low pressure separating zone, passing evolved vapors fromisaid separating zone to a fractionating operation wherein heavier constituents of said vapors are condensed as reilux condensate and thereby separated from desired lighter constituents of said vapors, withdrawing said reilux condensate from said fractionating operation and forcing it through said coil whereby it is subjected to cracking and subseguently passed to said vaporizing zone. Ysimultaneously passing another oil through a separate coil exposed to combustion' gases employed in heating said first-named coil and heating it during its ilow therethrough to a distilling 4temperature, discharging the'heated oil from the latter coil into a separate combined vaporizlng and fractionating zone wherein higher boiling constituents of said oil are separated and collected in liquid form and desired lower boiling constituents are separated in vapor form, separately withdrawing the said separated desired low boiling products,

' and Awithdrawing from the latter vaporlzing and fractionating operation separated higher boilingliquid products and introducing at least a portion vof them at below cracking temperature into the stream of cracked `products issuing from said first-named coil prior to their discharge into said first-named separating none to prevent overcra'cking of the said stream of cracked products.

11'. 'A continuous process for cracking and distilling oil which comprises heating oil under presrelatively hot section of a furnace, passing the oil from the coil into a separating zone wherein vapors and liquid residues are separated, fractionating and condensing the separated vapors andV withdrawing the condensate, heating and vaporizing anotler oil in another coil in a relatively cooler section of said furnace, fractionating the vsaid second mentioned oil and separately withdrawing a residuum, a condensate and lower boiling hydrocarbon vapors, collecting the low boiling hydrocarbon vapors and injecting a portion of said condensate into the outlet of the nal passes of the first mentioned coil to prevent overcrackf -ing of the hot oil therein.' c.

12. A continuous process for cracking and distilling oil which comprises heating oil under pressure to a cracking temperature in a coil in the relatively hot section of a furnace, passing the oil from the coil into a separating zone wherein vapors and liquid residues are separated, fractionating and condensing the separated .vapors and withdrawing the condensate, heating and vaporizing anotherA oil in another coil in another section of said furnace, fractionating the second mentioned oil to `separate it into a plurality of fractions' and injecting a portion-of a heavier fraction of the said second mentioned oil at below substantial cracking temperature into theoutlet of the ilnal passes of the first mentioned coil to prevent over-cracking of the hot oil, and cracking the injected oil by raising its temperature Asuddenly to a cracking degree.

13. The fprocess 'of' distilling and converting 25 hydrocarbon oils which comprises passing hydro- 'carbon oil through a pipe coll heated by hot gases of combustion wherein it is subjected to cracking under a relatively high pressure, discharging the cracked highly heated oil from said coil into a relatively low pressure separating zone, passing evolved vaporsfrom said separating zone to a fractionat-ing operation wherein heavier constituentsof said vapors areA condensed as reux condensate and thereby separated from desired lighter constituents of said vapors. simultaneously passing another oil through a separate coil exposed to combustion gases employed in heating Y said first-named coil and heating it during its ilow therethrough to a distilling temperature,l ,dischargingthe heated oil-from the latter coil into a separating zone, passing separated vapors from the latter zone to a fractionating zone wherein higher boiling constituents thereof are separated as ref luxcondensate, combining the latter reilux condensate with the said reflux condensate from said cracked vapors,` passing a portion ot the condensate mixture through said cracking coil as charging stock therefor, and introducing another portion of said condensate mixture atbelow substantial cracking temperature into the stream of cracked products issuing from said cracking coil prior to their discharge into said low pressure separating zone. A

somt c. BLACK. 

